WO2020100463A1

WO2020100463A1 - Hydrogen production apparatus

Info

Publication number: WO2020100463A1
Application number: PCT/JP2019/039389
Authority: WO
Inventors: 晃平江口; 拓人櫛; 広基飯沼
Original assignee: 東京瓦斯株式会社
Priority date: 2018-11-12
Filing date: 2019-10-04
Publication date: 2020-05-22
Also published as: JP6553273B1; JP2020079178A

Abstract

Provided is a hydrogen production apparatus provided with: a reformer which generates reformed gas containing a hydrocarbon as a main component by reforming hydrogen and to which the hydrocarbon is supplied as a raw material from a hydrocarbon supply source; a pressure increasing part that is connected to the reformer and that increases the pressure of the reformed gas; a hydrogen purifier that is connected to the pressure increasing part and that purifies a product hydrogen by separating the reformed gas into the product hydrogen and an off-gas being an impurity; a refrigerant-noncirculation-type first heat exchanger which is provided in a reformed gas flow path connecting the reformer and the pressure increasing part and in which the reformed gas is cooled through heat exchange with a refrigerant; and a refrigerant-circulation-type second heat exchanger which is provided in the reformed gas flow path on the downstream side of the first heat exchanger and in which the reformed gas is cooled through heat exchange with the refrigerant and water vapor contained in the reformed gas is condensed.

Description

Hydrogen production equipment

The present disclosure relates to a hydrogen production apparatus, for example, a hydrogen production apparatus that reforms a hydrocarbon raw material to produce hydrogen.

Conventionally, as a hydrogen production device for obtaining hydrogen, a PSA (Pressure Swing Adsorption) device, that is, a device for supplying hydrogen to a hydrogen purifier after reforming a raw material hydrocarbon into a reformed gas by a steam reforming device is known. ing. At this time, in order to supply the reformed gas to the PSA device at a pressure necessary for the adsorption reaction in the PSA device, a compressor for compressing the reformed gas is provided upstream of the PSA device.

Further, for example, as disclosed in JP-A-2017-88490, a chiller is provided on the upstream side of the compressor in the reformed gas flow path. This is the gas supplied to the compressor by cooling the reformed gas supplied to the compressor to condense steam, removing steam from the reformed gas, and then supplying the reformed gas to the compressor. It is excellent in that it reduces the flow rate and the load on the compressor.

However, if the reformed gas supplied to the compressor is cooled, that is, the steam is condensed only by the chiller, there is a disadvantage that the chiller has a large cooling load and the chiller for circulating the refrigerant becomes large.

That is, there was room for improvement in terms of downsizing of the hydrogen production equipment.

The present disclosure is to provide a hydrogen production device that is downsized while ensuring the cooling capacity of the reformed gas.

A first aspect of the present disclosure is a reformer that supplies hydrocarbon as a raw material from a hydrocarbon supply source and that reforms the hydrocarbon to generate a reformed gas containing hydrogen as a main component. A hydrogen booster connected to a reformer and boosting the reformed gas, and a hydrogen purifier connected to the booster and separating the reformed gas into product hydrogen and off gas which is an impurity to purify product hydrogen. A first non-refrigerant heat exchanger provided on a reformed gas flow path connecting the reformer and the booster unit and cooled by heat exchange of the reformed gas with a refrigerant; Refrigerant circulation provided on the reformed gas flow path downstream of the first heat exchanger to cool the reformed gas by exchanging heat with the refrigerant and to condense the water vapor contained in the reformed gas. And a second heat exchanger of the mold.

In this hydrogen production device, the first heat exchanger and the second heat exchanger are arranged from the upstream side on the reformed gas flow path through which the reformed gas flows from the reformer to the booster section. That is, the high-temperature reformed gas generated in the reformer is cooled by heat exchange with the refrigerant in the first heat exchanger and then cooled by heat exchange with the refrigerant in the second heat exchanger. The water vapor contained in the reformed gas is condensed and removed, and is supplied to the pressurizing unit.

That is, since the reformed gas is supplied to the second heat exchanger after being cooled by the first heat exchanger, the reformed gas supplied to the second heat exchanger has a relatively low temperature. For this reason, the cooling load of the second heat exchanger is relatively small as compared with the case where the reformed gas supplied to the booster is cooled only by the second heat exchanger.

That is, the refrigerant circulation type second heat exchanger can be downsized.

Also, the first heat exchanger is a non-refrigerant type in which a refrigerant is supplied from the outside of the hydrogen production apparatus and the heat-exchanged refrigerant is discharged to the outside of the hydrogen production apparatus. Therefore, upsizing of the hydrogen production device due to the addition of the first heat exchanger is suppressed.

As a result, compared with the case where the reformed gas introduced into the booster is cooled only by the second heat exchanger, the hydrogen production device can be downsized while ensuring a predetermined cooling capacity.

In the second aspect of the present disclosure, in the first aspect, the refrigerant used in the first heat exchanger may be industrial water.

In this hydrogen production device, if industrial water is used as the refrigerant of the first heat exchanger, the first heat exchanger can be easily installed in the hydrogen production device by simply connecting the industrial water supply source and the first heat exchanger. can do. That is, the hydrogen production device can be downsized while ensuring a predetermined cooling capacity with a simple configuration.

Note that industrial water includes not only industrial water supplied from industrial water supply, but also water supplied from wells, the sea, rivers, etc. and water supplied from tap water.

According to the above aspect, the hydrogen production device of the present disclosure can achieve downsizing of the device while ensuring the cooling capacity of the reformed gas.

It is a schematic block diagram which showed the hydrogen production apparatus which concerns on one Embodiment. It is a sectional view showing a multi-cylinder type reformer concerning one embodiment.

An example of a hydrogen production device according to an embodiment of the present disclosure will be described with reference to FIGS. 1 and 2.

<Hydrogen production equipment>
As shown in FIG. 1, the hydrogen production device 10 is a multi-cylinder reformer (hereinafter, may be referred to as a “reformer”) that produces a reformed gas obtained by steam reforming hydrocarbons, for example, city gas. 12, a compressor 80 for compressing the reformed gas, and a hydrogen purifier 90 for purifying hydrogen gas by removing impurities from the compressed reformed gas. Further, the hydrogen production device 10 includes a pre-pressurization water separation unit 50, a post-pressurization water separation unit 60, which separates and removes water from the reformed gas on the upstream side and the downstream side of the compressor 80, respectively, and the reformer 12 to be described later. And a combustion exhaust gas water separation unit 70 for separating and removing water from the combustion exhaust gas.

Further, the hydrogen production device 10 includes a heat exchanger HE1 and a chiller 100 between the reformer 12 and the pre-pressurization water separation unit 50, and a chiller 110 between the compressor 80 and the post-pressurization water separation unit 60. There is.

The hydrogen production device 10 produces hydrogen from a hydrocarbon raw material, and in the present embodiment, a case where city gas containing methane as a main component is used as an example of the hydrocarbon raw material will be described.

(Multiple cylinder reformer)
As shown in FIG. 2, the multi-tubular reformer 12 has a plurality of

tubular walls

21, 22, 23, 24 (hereinafter, may be referred to as “cylindrical walls 21-24”) arranged in multiple layers. Have The plurality of cylindrical walls 21 to 24 are formed in, for example, a cylindrical shape or an elliptic cylindrical shape. A combustion chamber 25 is formed inside the first cylindrical wall 21 from the inner side among the plurality of cylindrical walls 21 to 24, and a burner 26 is arranged downward on the combustion chamber 25. There is. The multi-tubular reformer 12 is an example of a reformer.

Further, an air supply pipe 40 for supplying combustion air from the outside is connected to the upper end of the combustion chamber 25. A raw material branch pipe 33A branched from a raw material supply pipe 33 for further supplying city gas is connected to the burner 26. An air branch pipe 40A branched from the air supply pipe 40 is connected to the raw material branch pipe 33A. An offgas recirculation pipe 120 is connected to the burner 26. Therefore, the burner 26 is configured to be supplied with gas in which city gas is mixed with air or off gas.

A combustion exhaust gas passage 27 is formed between the first tubular wall 21 and the second tubular wall 22. A lower end portion of the combustion exhaust gas passage 27 communicates with the combustion chamber 25, and a gas exhaust pipe 28 for exhausting gas is connected to an upper end portion of the combustion exhaust gas passage 27. The combustion exhaust gas discharged from the combustion chamber 25 flows from the lower side to the upper side in the combustion exhaust gas flow path 27 and is sent to the combustion exhaust gas water separation unit 70 through the gas discharge pipe 28.

Also, a first flow path 31 is formed between the second tubular wall 22 and the third tubular wall 23. An upper portion of the first flow passage 31 is formed as a preheating flow passage 32, and a raw material supply pipe 33 for supplying city gas and reforming water are supplied to an upper end portion of the preheating flow passage 32. Is connected to the reforming water supply pipe 34. Further, a spiral member 35 is provided between the second cylindrical wall 22 and the third cylindrical wall 23, and the preheating flow passage 32 is formed in a spiral shape by the spiral member 35. There is.

The city gas can be supplied to the preheating channel 32 from the raw material supply pipe 33, and further the reforming water can be supplied from the reforming water supply pipe 34. The city gas and the reforming water flow from the upper side to the lower side in the preheating channel 32, and are heat-exchanged with the combustion exhaust gas through the second cylindrical wall 22 to vaporize the water. In the preheating channel 32, the city gas and the reforming water in the vapor phase, that is, the steam are mixed to generate a mixed gas.

A reforming catalyst layer 36 is provided below the preheating channel 32 in the first channel 31, and the mixed gas generated in the preheating channel 32 is supplied to the reforming catalyst layer 36. It is a configuration. The reforming catalyst layer 36 receives heat from the combustion exhaust gas flowing through the combustion exhaust gas passage 27 and undergoes a steam reforming reaction of the mixed gas to generate a reformed gas containing hydrogen as a main component.

Furthermore, a second flow path 42 is formed between the third cylindrical wall 23 and the fourth cylindrical wall 24. The lower end of the second flow path 42 communicates with the lower end of the first flow path 31. A lower portion of the second flow passage 42 is formed as a reformed gas flow passage 43, and a reformed gas discharge pipe 44 is connected to an upper end portion of the second flow passage 42.

Further, a CO shift conversion catalyst layer 45 is provided above the reformed gas passage 43 in the second passage 42, and the reformed gas generated in the reformed catalyst layer 36 is the reformed gas flow. After passing through the passage 43, it is supplied to the CO shift catalyst layer 45. In the CO conversion catalyst layer 45, carbon monoxide and water vapor contained in the reformed gas are converted into hydrogen and carbon dioxide by an aqueous shift reaction, and carbon monoxide can be reduced.

Further, an oxidant gas supply pipe 46 is connected to the upper side of the CO shift catalyst layer 45, and a CO selective oxidation catalyst layer 47 is provided above the CO shift catalyst layer 45 in the second flow path 42. ing. The oxidizing gas introduced through the oxidizing gas supply pipe 46 and the reformed gas that has passed through the CO shift catalyst layer 45 are supplied to the CO selective oxidation catalyst layer 47. In the CO selective oxidation catalyst layer 47, carbon monoxide reacts with oxygen and is converted into carbon dioxide on a noble metal catalyst such as platinum or ruthenium, and carbon monoxide can be removed. The reformed gas G1 in which carbon monoxide is reduced in the CO shift catalyst layer 45 and the CO selective oxidation catalyst layer 47 is discharged through the reformed gas discharge pipe 44.

As shown in FIG. 1, the reformed gas generated in the multi-tubular reformer 12 passes through the pre-pressurization water separation unit 50, the compressor 80, the post-pressurization water separation unit 60, and the hydrogen purifier 90 in this order. Flowing. That is, in the gas flow direction, from the upstream side to the downstream side, the multi-tubular reformer 12, the pre-pressurization water separation unit 50, the compressor 80, the post-pressurization water separation unit 60, and the hydrogen purifier 90 are arranged in this order. It is arranged.

(Pre-pressurization water separator)
The downstream end of a reformed gas discharge pipe 44, into which the reformed gas G1 flows from the multi-cylinder reformer 12, is connected to the pre-pressurization water separation unit 50. A water recovery pipe 59 is connected to the bottom of the pre-pressurization water separation unit 50, and a communication flow path pipe 56 is connected to the top of the pre-pressurization water separation unit 50. The reformed gas G1 is separated by condensing water by cooling by heat exchange with a refrigerant in a heat exchanger HE1 and a chiller 100 which are arranged in a reformed gas discharge pipe 44 upstream of the pre-pressurization water separation unit 50. The liquid-phase water can be stored under the pre-pressurization water separation unit 50. The liquid phase water is sent to the water recovery pipe 59. The reformed gas G2 after the water is condensed is sent to the communication flow path pipe 56. The reformed gas discharge pipe 44 corresponds to the “reformed gas passage”.

(Heat exchanger)
The heat exchanger HE1 is connected to an industrial water supply pipe 51 that communicates with an industrial water supply source outside the hydrogen production device 10 and an industrial water discharge pipe 52 that communicates with the outside of the hydrogen production device 10. Therefore, in the heat exchanger HE1, the industrial water supplied from the industrial water supply pipe 51 is heat-exchanged with the reformed gas G1, that is, the reformed gas is cooled, and the industrial water after the heat exchange is the industrial water discharge pipe 52. It is configured to be discharged to the outside of the hydrogen production device 10 through the. The heat exchanger HE1 corresponds to the “first heat exchanger”. Further, the industrial water corresponds to the "refrigerant" of the first heat exchanger.

(Chiller)
The chiller 100 is located on the reformed gas exhaust pipe 44 downstream of the heat exchanger HE1. As shown in FIG. 1, the heat exchange section 102 disposed on the reformed gas exhaust pipe 44, the radiator 104 disposed at a position separated from the heat exchange section 102, the heat exchange section 102 and the radiator 104. And a chiller water circulation channel 106 through which chiller water is circulated.

A pump 107 for circulating the chiller water is arranged in the chiller water circulation passage 106. Further, the radiator 104 is provided with a fan 108 for cooling the chiller water that has become high temperature due to heat exchange in the heat exchange section 102.

That is, the chiller water cooled in the radiator 104 is supplied to the heat exchange section 102 via the chiller water circulation flow path 106 and exchanges heat with the reformed gas flowing through the reformed gas discharge pipe 44, that is, the reformed gas is generated. The structure is cooled. The chiller 100 corresponds to the "second heat exchanger". The chiller water corresponds to the "refrigerant" of the second heat exchanger.

(Compressor)
In the compressor 80, there are a communication flow passage pipe 56 through which the reformed gas G2 from the pre-pressurization water separation unit 50 flows, and a communication flow passage pipe 66 through which the reformed gas G2 supplied to the post-pressurization water separation unit 60 flows. It is connected. The compressor 80 is capable of compressing the reformed gas G2 supplied from the pre-pressurization water separation unit 50 and supplying it to the post-pressurization water separation unit 60. In addition, the compressor 80 corresponds to a “pressure booster”.

(Water separation unit after pressurization)
To the post-pressurization water separation unit 60, a downstream end of a communication flow pipe 66 that allows the reformed gas G2 to flow from the compressor 80 is connected. A water recovery pipe 69 is connected to the bottom of the post-pressurization water separation unit 60, and a communication channel pipe 68 is connected to the top of the post-pressurization water separation unit 60. The reformed gas G2 is separated and condensed in a chiller 110, which will be described later, disposed in the communication flow path pipe 66 upstream of the post-pressurization water separation unit 60 by cooling by heat exchange with a refrigerant, that is, chiller water. After the pressurization, liquid phase water can be stored in the lower part of the water separation unit 60. The liquid phase water is sent to the water recovery pipe 69. The reformed gas G3 after the water is condensed is sent to the communication flow path pipe 68.

(Chiller)
Like the chiller 100, the chiller 110 includes a heat exchange section 112, a radiator 114, a chiller water circulation passage 116, and a pump 117. In addition, the radiator 114 is provided with a fan 118, like the radiator 104.

(Hydrogen refiner)
The hydrogen purifier 90 is connected to the downstream end of the communication flow pipe 68 through which the reformed gas G3 from the post-pressurization water separation unit 60 flows and the upstream end of the offgas reflux pipe 120 through which the offgas of the hydrogen purifier 90 flows. ing.

As the hydrogen purifier 90, a PSA device is used as an example. The hydrogen purifier 90 includes a pair of adsorption tanks, one adsorption tank performs an adsorption step of adsorbing impurities on the adsorbent, and the other adsorption tank performs a desorption step of desorbing the impurities adsorbed on the adsorbent, Next, the desorption process is performed in one adsorption tank, and the adsorption process is performed in the other adsorption tank. By repeating this periodically, the reformed gas G3 is continuously separated into hydrogen and impurities containing carbon monoxide, that is, off-gas OG, and hydrogen is purified. The purified hydrogen is sent to the hydrogen supply pipe 92, can be stored in a tank (not shown), or can be sent to the hydrogen supply line.

The off gas of the hydrogen purifier 90 can be supplied to the burner 26 of the reformer 12 via the off gas reflux pipe 120. It should be noted that the off-gas tank 122 for temporarily storing the off-gas on the off-gas recirculation pipe 120 and flowing the same to the burner 26 to equalize the composition and flow rate of the off-gas supplied from the hydrogen purifier 90 and supply the off-gas to the burner 26. Is provided.

(Combustion exhaust gas water separation unit)
The downstream end of a gas exhaust pipe 28 that guides the combustion exhaust gas from the combustion exhaust gas flow path 27 of the reformer 12 is connected to the combustion exhaust gas water separation unit 70. A water recovery pipe 78 is connected to the bottom of the combustion exhaust gas water separation unit 70, and a gas discharge pipe 76 is connected to the upper portion of the combustion exhaust gas water separation unit 70. The combustion exhaust gas discharged from the combustion chamber 25 is separated and condensed in the heat exchanger HE3 arranged in the gas discharge pipe 28 upstream of the combustion exhaust gas water separation unit 70 by cooling by heat exchange with cooling water. The liquid water can be stored under the combustion exhaust gas water separation unit 70. The liquid phase water is sent to the water recovery pipe 78. The combustion exhaust gas after the water is condensed is discharged from the gas discharge pipe 76 into the outside air.

The downstream end of each of the

water recovery pipes

59, 69, 78 is connected to the reforming water supply pipe 34. The reforming water supply pipe 34 is provided with a water treatment device 34A made of an ion exchange resin for removing dissolved ion components. The external water supply unit 17 is connected to the reforming water supply pipe 34. For example, pure water or city water is supplied from the external water supply unit 17 to the reforming water supply pipe 34.

Further, the reforming water supply pipe 34 is provided with a pump P1. The water separated by the pre-pressurization water separation unit 50, the post-pressurization water separation unit 60, the combustion exhaust gas water separation unit 70, or the water supplied from the external water supply unit 17 is sent to the multi-tubular reformer 12 by the pump P1. It is a configuration to be supplied.

(Action)
Next, the operation of the hydrogen production device 10 will be described.

City gas is supplied from the raw material supply pipe 33 to the multi-cylinder reformer 12. As shown in FIG. 2, the city gas supplied to the multi-cylinder reformer 12 is heated while being mixed with the reforming water in the preheating channel 32 of the multi-cylinder reformer 12, and the reforming catalyst It is supplied to the layer 36. In the reforming catalyst layer 36, the mixed gas receives heat from the combustion exhaust gas flowing through the combustion exhaust gas passage 27 to cause a steam reforming reaction, and a reformed gas containing hydrogen as a main component is generated. The reformed gas is supplied to the CO shift catalyst layer 45 through the reformed gas passage 43. In the CO conversion catalyst layer 45, carbon monoxide contained in the reformed gas reacts with steam to be converted into hydrogen and carbon dioxide, and carbon monoxide is reduced.

Further, the reformed gas that has passed through the CO conversion catalyst layer 45 is supplied to the CO selective oxidation catalyst layer 47 together with the oxidizing gas (air) supplied from the oxidizing gas supply pipe 46, and carbon monoxide is converted into oxygen on the precious metal catalyst. Reacts with and is converted to carbon dioxide, and carbon monoxide is removed. The reformed gas G1 in which carbon monoxide is reduced in the CO selective oxidation catalyst layer 47 is sent to the reformed gas discharge pipe 44.

At this time, in the combustion chamber 25 of the multi-cylinder reformer 12, a gas obtained by mixing the city gas and air supplied from the raw material branch pipe 33A and the air branch pipe 40A or an off gas supplied from the off gas recirculation pipe 120. Are burned by the burner 26. The combustion exhaust gas is supplied from the combustion chamber 25 to the combustion exhaust gas water separation unit 70 via the combustion exhaust gas flow passage 27 and the gas exhaust pipe 28. As shown in FIG. 1, the water contained in the combustion exhaust gas is cooled and condensed by heat exchange in the heat exchanger HE3, stored in the combustion exhaust gas water separation unit 70, and sent to the water recovery pipe 78. The combustion exhaust gas from which the water has been separated is discharged from the gas discharge pipe 76 into the outside air.

On the other hand, as shown in FIG. 1, the reformed gas G1 is heated to a high temperature, for example, 100 ° C. in the reformer 12 by a steam reforming reaction or an aqueous shift reaction. The reformed gas G1 flowing through the reformed gas discharge pipe 44 is first heat-exchanged with industrial water by the heat exchanger HE1 and cooled to, for example, 32 ° C. The reformed gas G1 cooled in the heat exchanger HE1 is further heat-exchanged with the chiller water in the heat exchange section 102 of the chiller 100, and further cooled to, for example, 10 ° C.

As a result, the reformed gas G1 flowing through the reformed gas discharge pipe 44 is cooled by the heat exchanger HE1 and the chiller 100, so that the steam is condensed.

The reformed gas G1 is supplied to the pre-pressurization water separation unit 50 via the reformed gas discharge pipe 44. In the pre-pressurization water separation unit 50, water condensed by cooling by heat exchange in the heat exchanger HE1 and the chiller 100 is stored and sent to the water recovery pipe 59. The reformed gas G2 from which the water has been separated is supplied to the compressor 80 from the communication flow path pipe 56 and is compressed by the compressor 80.

The compressed reformed gas G2 is supplied to the water separation unit 60 after pressurization from the communication flow pipe 66. In the post-pressurization water separation unit 60, water condensed by cooling by heat exchange in the chiller 110 is stored and sent to the water recovery pipe 69. The reformed gas G3 from which water has been separated is supplied to the hydrogen purifier 90 from the communication flow path pipe 68.

The water sent from the pre-pressurization water separation unit 50, the post-pressurization water separation unit 60, and the combustion exhaust gas water separation unit 70 to the

water recovery pipes

59, 69, and 78 is returned to the reforming water supply pipe 34. By driving the pump P1, the reforming water supply pipe 34 supplies the reforming water to the multi-cylinder reformer 12.

The hydrogen purifier 90 employs a pressure swing method, in which one of the pair of adsorption tanks adsorbs impurities other than hydrogen in the adsorbent and the other adsorption tank desorbs the impurities adsorbed in the adsorbent. .. In the hydrogen purifier 90, the adsorption step and the desorption step are repeated in each adsorption tank at a constant cycle to continuously separate hydrogen and impurities from the reformed gas G3 to purify hydrogen.

Hydrogen as a product purified by the hydrogen purifier 90 is sent to the hydrogen supply pipe 92, stored in a tank (not shown), or sent to the hydrogen supply line.

On the other hand, the off-gas OG discharged from the hydrogen purifier 90 flows through the off-gas recirculation pipe 120, is temporarily stored in the off-gas tank 122, and is then stored in the burner 26 provided in the combustion chamber 25 of the reformer 12 in terms of flow rate and composition. Is leveled and supplied.

As described above, in the hydrogen production device 10, the high temperature reformed gas G1 sent from the reformer 12 is first cooled by the heat exchanger HE1 and then cooled by the chiller 100 on the reformed gas discharge pipe 44. Water is supplied to the pre-pressurization water separation unit 50 to separate condensed water from the reformed gas G1.

That is, since the heat exchanger HE1 is provided on the upstream side of the chiller 100, the cooling load of the chiller 100 is reduced, and the chiller 100 can be downsized.

The heat exchanger HE1 is for exchanging heat between the industrial water supplied to the factory and the reformed gas G1, and the industrial water is supplied from an industrial water supply source outside the hydrogen production apparatus 10 to perform heat exchange. The industrial water is a refrigerant non-circulation type that is discharged to the outside of the hydrogen production apparatus 10. Therefore, the heat exchanger HE1 is smaller than the refrigerant circulation type heat exchanger, and an increase in the size of the hydrogen production device 10 due to the addition of the heat exchanger HE1 is suppressed.

In particular, the heat exchanger HE1 is provided with an industrial water supply pipe 51 and an industrial water discharge pipe 52 except for the portion where the reformed gas G1 and the industrial water exchange heat, and the industrial water supply pipe 51 is connected to the outside of the hydrogen production apparatus 10. Since it suffices to connect it to the industrial water supply source described above, it has a simple structure and further suppresses the increase in size of the hydrogen production device 10 due to the provision of the heat exchanger HE1.

Therefore, as compared with the case where the refrigerant circulation type chiller alone is used for cooling, the combination of the refrigerant non-circulation type heat exchanger HE1 and the refrigerant circulation type chiller 100 can reduce the size of the hydrogen production device 10. You can

On the other hand, since the industrial water used in the heat exchanger HE1 is, for example, about 32 ° C., the reformed gas G1 discharged from the reformer 12 can be sufficiently cooled at a high temperature, for example, 100 ° C. That is, a predetermined cooling capacity can be secured by combining the non-refrigerant heat exchanger HE1 and the downsized refrigerant circulation chiller 100.

As described above, the hydrogen production device 10 secures (maintains) the cooling capacity as compared with the case where the reformed gas G1 supplied to the compressor 80 (pre-pressurizing water separation unit 50) is cooled by a single chiller. It can be miniaturized.

Further, when industrial water is already used at the installation location of the hydrogen production device 10, it is possible to easily cool it by the heat exchanger HE1 by only supplying a part of this industrial water to the heat exchanger HE1. Become.

[Other]
In the hydrogen production device 10 according to the present embodiment, the heat exchanger HE1 in which industrial water exchanges heat with the reformed gas G1 is described as a refrigerant non-circulation type heat exchanger, but the present invention is not limited to this. For example, it may be a heat exchanger that utilizes the cold heat of liquefied natural gas.

Also, for example, an air fin cooler that exchanges heat with the reformed gas G1 may be used. In this case, a part of the reformed gas discharge pipe 44 is branched into a large number of pipes, air that is a refrigerant is introduced from the outside of the hydrogen production apparatus 10 and blown to this branched portion to cool the reformed gas G1. At the same time, the heat-exchanged air may be discharged to the outside of the hydrogen production device 10.

That is, the refrigerant non-circulation type heat exchanger may be any one as long as the refrigerant is supplied from the outside of the hydrogen producing apparatus 10 and the heat-exchanged refrigerant is discharged to the outside of the hydrogen producing apparatus 10.

Further, the industrial water of the present embodiment includes not only industrial water supplied from the industrial water supply, but also water supplied from wells, the sea, rivers, etc. and water supplied from the tap water.

In the hydrogen production device 10 according to the embodiment, the reformer 12 is a multi-cylinder reformer, but the invention is not limited to this. It is only necessary that the city gas can be reformed into a reformed gas containing hydrogen as a main component.

Further, in the hydrogen production device 10 according to the embodiment, the case where the hydrogen purifier 90 is a PSA device has been described, but the hydrogen purifier 90 is not limited to this as long as hydrogen can be purified from the reformed gas G3.

Further, in the hydrogen production device 10 according to the embodiment, the CO shift conversion catalyst layer 45 and the CO selective oxidation catalyst layer 47 are provided in order to remove carbon monoxide from the reformed gas in the reformer 12, You may comprise only the CO conversion catalyst layer 45.

Further, in the hydrogen production apparatus according to the embodiment, the compressor 80 has been described as an example of the pressure increasing unit, but if the pressure is high and the reformed gas G2 is supplied to the hydrogen purifier 90, the present invention is not limited thereto. Absent.

The disclosure of Japanese Patent Application 2018-212518 dated November 12, 2018 is incorporated herein by reference in its entirety.

All publications, patent applications, and technical standards mentioned herein are to the same extent as if each individual publication, patent application, and technical standard were specifically and individually noted to be incorporated by reference, Incorporated herein by reference.

Claims

A hydrocarbon is supplied as a raw material from a hydrocarbon supply source, and a reformer that reforms the hydrocarbon to generate a reformed gas containing hydrogen as a main component,
A booster connected to the reformer and boosting the reformed gas;
A hydrogen purifier that is connected to the booster unit and that purifies the product hydrogen by separating the reformed gas into product hydrogen and off gas that is an impurity,
A first heat exchanger of a refrigerant non-circulation type, which is provided on a reformed gas flow path connecting the reformer and the booster, and is cooled by heat exchange of the reformed gas with a refrigerant,
A refrigerant provided on the reformed gas passage downstream of the first heat exchanger and cooled by heat exchange of the reformed gas with a refrigerant to condense steam contained in the reformed gas. A circulation type second heat exchanger,
Hydrogen production device equipped with.
The hydrogen generator according to claim 1, wherein the refrigerant used in the first heat exchanger is industrial water.